WO1980001103A1 - Recuperation de chaleur et de liquide utilisant un systeme a pompe de chaleur a cycle ouvert - Google Patents

Recuperation de chaleur et de liquide utilisant un systeme a pompe de chaleur a cycle ouvert Download PDF

Info

Publication number
WO1980001103A1
WO1980001103A1 PCT/US1979/000976 US7900976W WO8001103A1 WO 1980001103 A1 WO1980001103 A1 WO 1980001103A1 US 7900976 W US7900976 W US 7900976W WO 8001103 A1 WO8001103 A1 WO 8001103A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
heat exchange
heat
expansion
temperature
Prior art date
Application number
PCT/US1979/000976
Other languages
English (en)
Inventor
B Fox
Original Assignee
Minnesota Mining & Mfg
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Minnesota Mining & Mfg filed Critical Minnesota Mining & Mfg
Priority to BR7908908A priority Critical patent/BR7908908A/pt
Priority to DE7979901646T priority patent/DE2967226D1/de
Publication of WO1980001103A1 publication Critical patent/WO1980001103A1/fr

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
    • F26B25/005—Treatment of dryer exhaust gases
    • F26B25/006—Separating volatiles, e.g. recovering solvents from dryer exhaust gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B23/00—Heating arrangements
    • F26B23/001—Heating arrangements using waste heat
    • F26B23/002—Heating arrangements using waste heat recovered from dryer exhaust gases
    • F26B23/004—Heating arrangements using waste heat recovered from dryer exhaust gases by compressing and condensing vapour in exhaust gases, i.e. using an open cycle heat pump system
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
    • Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
    • Y02B30/52—Heat recovery pumps, i.e. heat pump based systems or units able to transfer the thermal energy from one area of the premises or part of the facilities to a different one, improving the overall efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • solvents are commonly used in the coating dispersions or solutions to permit transfer and application of the coating.
  • the coated web or article is often passed through an oven where the solvent is evaporated and the coating dried and cured.
  • Sufficient air is passed through the oven to prevent the accumu ⁇ lation of excessive solvent vapor. if the solvent is combustible, enough fresh air is circulated through the oven to keep the solvent vapor concentration well below the lower explosive limit (L.E.L.).
  • Oven gas temperatures are often in the range of 40° C - 200° C. Discharging the gas passing through the oven therefore represents a substantial energy loss in the hot exhaust gas as well as a loss of the evapor ⁇ ated solvent vapors. It is therefore desirable to be able to recover the solvent and/or heat contained in the gas discharged from the oven.
  • solvent recovery means presently used is a carbon adsorption system. Solvent laden air is passed through an activated carbon bed where the solvent vapors are adsorbed on to the surface of the carbon. When the carbon bed becomes saturated, or nearly so, the carbon is desorbed by passing steam through the carbon bed. The solvent and steam are then condensed and the solvent and water separated by decanting or by distillation. In practice, two or more beds are used so that the operation may be continuous with one bed adsorbing solvent vapors while another is being desorbed.
  • Closed cycle vapor compression refrigeration systems are commonly used in the petroleum industry for cooling solvent vapors at high concentrations to cause condensation, but such systems are not widely used for recovering solvents in industrial manufacturing operations. Factors limiting their application for such use are: 1) The inability to reject heat from the condenser at sufficiently high enough temperature for use of the rejected heat in the oven; 2) The complexity of the machines required to obtain the necessary low temperatures to condense volatile solvent vapors at low concentrations, e.g. at concentrations below the L.E.L.; 3) Ice formation on the evaporator; and 4) Relatively low reliability and high maintenance costs.
  • V ⁇ IP ethod also requires about four to seven pounds of steam to desorb a pound of solvent. Approximately 1000 BTU's are required to generate one pound of steam.
  • the air passing over the condenser is cooled in the process of condensing the solvent vapors. Either this air or ambient air must be heated for return to the oven.
  • the latent heat of the condensed solvent vapors and the sensible heat from cooling of the air are rejected through the refrigeration condenser.
  • the present invention overcomes many of the disadvantages associated with the previously employed solvent recovery techniques by providing a novel means for condensing and recovering vapors from a gas,, while at the same time providing the capability of recovering heat and work from the vapor-containing gas, thereby providing an energy-efficient system.
  • the present invention also provides means for recovery of heat from a gas, particularly a process gas heated above the ambient, where the recovery of the vapor may or may not be desired.
  • open cycle heat pump system or "open cycle system” refers to a system wherein a working fluid is taken into the system, acted upon so as to change the pressure and temperature of the fluid to cause condensation of the condensable vapor contained therein, or advantageous heat transfer, and expelled.
  • the working fluid e.g., freon
  • the working fluid is sealed in a closed loop within the system and is continuously recycled to cool an air space by. heat transfer between the working fluid and the air space.
  • condensable vapor refers to materials which are normally liquid at room temperature, that is those materials which can be vaporized at temperatures normally encountered in industrial drying conditions, e.g. 20° C to 200° C whether at standard or reduced pressure, but which can exist as a liquid at temperatures at or near room temperature and at pressures at or near atmospheric pressure.
  • the term thus includes the commonly used industrial solvents which are used in coating resin formulations and the like and which can be flashed or vaporized in conventional industrial drying ovens.
  • the open, cycle system used in the recovery technique and apparatus described herein comprises an apparatus which operates on a working fluid to produce changes in pressure on the working fluid and, together with auxiliary cooling, if desired, causes selected vapors contained in the working fluid to condense.
  • the system can also include means for providing heat recovery where vapor may or may not be condensed and collected.
  • the open cycle system comprises, in sequence, means for compressing the working fluid, means for cooling the compressed fluid, means for expanding the compressed fluid to further cool the fluid and means for removing condensate from the system at points where condensation occurs.
  • the above system also comprises means for causing the expanded fluid to cool the compressed fluid prior to expansion.
  • the compression/ expansion sequence of the open cycle system may be reversed.
  • This system would comprise, in sequence. eans for expanding the working fluid to cool the fluid and cause condensation of the condensable vapor contained therein, means for removing the condensate at points where condensation occurs, and means for compressing said fluid to provide a pressure differential, for the expanderv—Since the function of the compressor is to provide a pressure differential for the expander, in theory it may either precede or follow the expander in sequence.
  • means for cooling of the fluid prior to expansion is not needed although such cooling may be effected, if desired.
  • the system also comprises means for utilizing the expanded. fluid to precool the fluid entering the expander.
  • a system to effect such removal might comprise, for example, a circulating-gas drying oven having an open cycle solvent recovery unit in combination therewith for removing vaporized solvent from the circulating gas.
  • Another aspect of the present invention relates to a method of recovering condensable vapor from a gas stream or gaseous atmosphere, wherein the vapor-containing gas is compressed, cooled by a heat exchange means and expanded to produce further cooling.
  • the cooled, expanded gas is then directed through a heat exchange means to effect pre-cooling of the compressed gas prior to expansion.
  • the condensed vapor is collected and removed at one or more points in the processing cycle.
  • Yet another aspect of the invention relates to the recovery of heat from a gas utilizing an open cycle heat pump system, wherein heat from the gas is transferred to gas entering or reentering the process.
  • the recovery of condensed vapor may or may not be important in such a process.
  • Air cycle heat pumps in a different arrangement than conceived in this invention, have been used for many years in environmental control, e.g. automobile air conditioning and the cooling of aircraft cabins, see for example U.S. Patents 3686893, 3877245 and 3886765.
  • the invention described herein is the first use of an open cycle heat pump system for industrial solvent and/or heat recovery.
  • FIGURE 1 is a schematic diagram of an open cycle heat pump system coupled to a working fluid.
  • FIGURE 2 is a schematic diagram of an apparatus according to the present invention comprising a circulating gas drying oven in combination with an open cycle heat pump system for solvent recovery.
  • FIGURE 3 is a schematic diagram of an alternative arrangement of an open cycle heat pump system particularly adapted for heat recovery from a working fluid.
  • FIG. 1 An open cycle heat pump system useful in the present invention is shown in Figure 1 and comprises, in combination, a compressor 1, heat exchanger 3, turbine or expander 5 and drive means 7 for the compressor 1, such as an electric motor.
  • the compressor 1, and the turbine 5 are coupled together in such a manner that the work produced by the turbine 5 is utilized to help drive the compressor 1, thus reducing the load on the drive motor and improving the overall efficiency of the system.
  • a working fluid in the form of a condensable vapor-laden gas, such as air, at nominally atmospheric pressure enters the recovery apparatus through inlet line 9 at temperature T ⁇ and pressure P ⁇ and is compressed by compressor 1 to T2 and P2 where the ratio of P2/P1 is generally about 1.3:1 to 3:1. Since the compression is essentially adiabatic, a working relationship which indicates the temperature rise can be expressed as
  • T 2 *2 (T) ⁇ l p l
  • n is a ratio of the constant pressure and constant volume specific heats of the working fluid and is about 1.4 for air.
  • the gas may leave the compressor at about 150° C. After leaving compressor 1, the gas passes through line 11, heat exchanger 3 and line 13, on its way to expander 5.
  • the precooled gas from heat exchanger 3 enters expander 5 where it expands back to nominal atmospheric pressure becoming cooled in the process according to the equation
  • T3 P3 The work produced during expansion is used to help drive compressor 1, thus reducing the load on drive motor 7.
  • some vapors may condense in heat exchanger 3 e ' nroute to expander 5.
  • a drain line 15 is provided to remove and collect any liquid that may condense. Additional vapor may condense on cooling during passage through expander 5 and exit line 17. This condensate is captured and collected by means of a condensate separator 19.
  • one or more ice traps, such as shown at 21, may be incorporated at one or more locations in the system in the event conditions exist which could cause ice formation in the working fluid.which would accumulate in the separator 19, heat exchanger 3 or elsewhere in the system.
  • the ice trap 21 can be omitted or bypassed.
  • the cooled gas can then be purged through line 23.
  • the cooled gas with much of the vapor condensed and removed exits the separator through line 25 and is returned to the working fluid stream or reservoir, generally at a point downstream from where withdrawn, via heat exchanger 3 and lines 27 and 29, where the gas is reheated to a temperature Tg approaching or even exceeding the original working fluid temperature T ⁇ _.
  • Heat exchanger 3 thus performs the dual function of precooling the gas enroute to expander 5 and reheating the cooled gas from expander 5, returning through line 25, before being returned to the working fluid stream or reservoir.
  • the gas exiting heat exchanger 3 may be heated to temperature T7 by auxiliary heater 31 to maintain the desired working fluid temperature. Further, a portion of the gas exiting heat exchanger 3 ay be purged through line 33 with corresponding make-up gas being provided through line 35 at a point in the system prior to or after auxilliary heater 31, as desired. Valves 37, 38 and 39 may be used to bleed off or add. make-up gas to the system, as may be desired. For example, if the condensable vapor contained in the gas is not valuable or otherwise need not be retained, the gas leaving condensate separator 19 may be vented through valve 39. By closing valve 38 and opening valve 37, ambient air or other gas may be passed through heat exchanger 3 to the process or working fluid reservoir via line 29. This arrangement allows recovery of heat from the gas entering line 9, even though the vapor, for example, water vapor, need not be recovered.
  • the compression and expansion means serves to temporarily alter the pressure and temperature of the gas passing therethrough so that the difference in temperature between the two quantities of gas entering the heat exchanger 3 is increased to promote heat transfer. In this way the temperature of the gas leaving the heat exchanger 3 through line 27 can be raised above the temperature of the gas entering the system through line 9.
  • gas can be returned to the process at the same or even higher temperature if desired.
  • the compressor and expander used in the present invention may be of any suitable type: reciprocating-, vane, rotary screw, centrifugal, axial flow, or other type.
  • High efficiency e.g. about 70% or greater, is desirable in order to minimize the net -10-
  • the pressure ratio of the compressor and expander is a design variable that can be selected to optimize any given application.
  • the greater the pressure ratio the greater the temperature change through the compressor and expander, but also the greater the net power required to drive the system.
  • a pressure ratio of up to about 4:1 with pressure ratios in the range of 1.3:1 to 3:1 being generally preferred as the most advantageous.
  • the compressor may be driven by an electric motor, gas turbine engine, steam turbine, or other suitable means.
  • the heat exchangers used in the open cycle system of the present invention can be any conventional type such as co-current, countercurrent, crossflow, gas-gas, gas-liquid, etc. It is desirable that the heat exchanger have an efficiency of about 70% or greater in order to enhance the economics of the process. Further, since the open cycle system described herein generally operates at relatively low pressure ratios, it is desirable that the pressure drop across the heat exchangers also be minimized to maintain efficiency. However, while the pressure drops must be minimized in a low pressure open cycle system, certain advantages also accrue in that the heat exchangers need not be hermetically sealed as with a closed cycle freon system and, due to the low pressures encountered, can be constructed, of light duty economical materials.
  • Any excess heat given off by the condensation of vapor entering in line 11 can be advantageously rejected to another sink to improve efficiency of the system.
  • this can be readily accomplished by the use of an auxiliary heat exchanger to extract heat from the gas entering in line 11 at some point inter ⁇ mediate heat exchanger 3.
  • This configuration takes advantage of the maximum temperature differences at each end of the exchanger in a counter current mode in order to obtain maximum heat transfer.
  • ice When operating conditions in the system are such that ice may form, e.g. when operating below 0° C with a solvent, such as heptane, which does not depress the freezing point of water, some means or technique may be necessary for preventing the formation of or for the removal of frost and ice from the separator, heat exchangers or other parts of the system. This may be no more than a dual set of heat exchangers permitting defrosting of one set while the other is operating, or means, such as a molecular sieve, may be used to remove the moisture before it has a chance to collect on the component surfaces. Yet another technique is to inject a small quantity of alcohol, or pther freezing point depressant, to depress the freezing point sufficiently to prevent frost or ice formation.
  • a solvent such as heptane
  • the separator shown generally at 19 in Figure 1, must perform the function of separating the condensed liquid droplets from the gas stream in which it is entrained.
  • Useful separators are well known in the art and can take the form of screens or packed columns which provide a large surface area on which the droplets can coalesce and drain away.
  • FIG. 2 there is shown a circulating gas oven 41 wherein a solvent-coated web 43 can be moved through the oven 41 counter to (shown) or in the same direction as the gas flowing through oven 41.
  • the gas may be a heated gas to aid in the solvent removal.
  • the solvent-coated web may be heated by other means to drive off the solvent, such as by radiation heating or conductive heating techniques.
  • the gas drying medium is introduced into the system through line 45 and enters the oven 41 where it passes over and around web 43, picking up solvent from the coating on web 43.
  • the gas drying medium then exits the oven 41 through line 47.
  • At least a portion of the solvent vapor-containing exit gas is fed through line 49 to a solvent recovery unit 53 while the remainder of the gas is recirculated to the oven entrance through line 51, blower 57, line 59, heater 61 and line 45-
  • a portion of the gas may be purged through line 63 with the desired amount of make-up gas provided through line 65.
  • the solvent recovery unit shown generally at 53 such as a unit shown in Figure 1, separates a portion of the condensable vapors from the gas and these are removed from the recovery unit 53 through line 67.
  • recovery unit 53 may also extract- heat from the gas medium entering recovery unit 53 and utilize the extracted heat to reheat the gas medium exiting the recovery unit through line 55, as has been discussed in greater detail with respect to Figure 1.
  • the desired drying gas velocity and temperature through oven 41 is provided by blower 57 and heater 61.
  • the amount of drying gas flowing through recovery unit 53 is a function of the size and speed of the compressor in recovery unit 53.
  • the recovery apparatus of this inven ⁇ tion When the recovery apparatus of this inven ⁇ tion is to be used in combination with a circulating gas drying oven and where the gas exiting the recovery apparatus is to be returned to the oven, it is not necessary to remove all the solvent vapors in each pass through the recovery apparatus.
  • the quantity of solvent vapor condensed for each unit of gas passing through the recovery apparatus and the volume rate of circulation are design trade-offs to be optimized for each particular installation.
  • the portion of gas to be circulated through recovery unit 53 will vary depending on various economic considerations.
  • the size of the components of recovery unit 53 will depend on the flow rate of gas which must be processed.
  • the cost of recovery unit 53 will depend to some extent on the size of the components.
  • the flow rate of gas which must be processed is influenced by the oven tempera ⁇ ture, oven web speed, solvent concentration, type, and costs. Thus, all of these are design factors which must be balanced in each case to obtain the most efficient process.
  • the unit is self-stabilizing to the extent that for a given working fluid flow rate, which will be a function of the size of the components, speed of compressor and turbine, etc., a change in concentration of condensable vapor entering the system causes a corresponding change in the amount of conden ⁇ sate removed from the working fluid. .
  • This is because the working fluid exiting the expander unit is always saturated with condensable vapor at the expanded temperature regardless of an increase in the concen- tration of condensable vapor in the working fluid entering the system.
  • the open cycle heat pump system may be operated so as to recover heat from a gas even though the vapor need not be retained or recovered.
  • the gas from which the heat has been recovered may be either recycled or vented, as desired.
  • Hot gas enters the system through line 71 and passes through heat exchanger 3 wherein heat is transferred to the gas entering the heat exchanger through line 85. Having cooled, and leaving the heat exchanger 3. through line 73 the gas, which may still contain vapor, may be vented through valve 75. After closing valve 79 in line 77, ambient air or other gas
  • OMPI may then be allowed to enter through valve 81 and line 83 where it is cooled in expander 5.
  • the cooled gas then flows through heat exchanger 3 where it is warmed by the gas entering through line 71.
  • the warmed gas is then further heated on passing through compressor 1 before entering the process or reservoir of heated gas through line 89.
  • the expansion and compression means serves to temporarily alter the pressure and temperature of the gas passing therethrough so that the difference in temperature between the two quantities of gas entering heat exchanger 3 is increased to promote heat transfer.
  • a drain line 91 is provided to remove condensate which may be formed in heat exchanger 3.
  • the gas exiting the heat exchanger through line 73 should not be vented, e.g. where the gas contains valuable or toxic vapor or where the temperature of the ambient air or other gas source is much lower than the temperature of the gas in line 73, then by appropriate adjustment of valves 75, 79 and 81 the gas can be recirculated through line 83 etc. as described above to be reheated and reenter the process or gas reservoir.
  • the work performed in the expander may be used to drive the compressor and improve the overall efficiency of the system.
  • the open cycle system can be designed to recover any common industrial solvent. Considerations for the recovery of heptane vapor (a common industrial solvent) are discussed hereinafter followed by a review of typical operating conditions encountered in an actual test unit.
  • the lower explosive limit (L.E.L.) for heptane vapor in air is 1.05 percent by volume. This corresponds to a vapor pressure of.7.98 millimeters of mercury in air at normal atmospheric pressure.
  • L.E.L. The lower explosive limit for heptane vapor in air is 1.05 percent by volume. This corresponds to a vapor pressure of.7.98 millimeters of mercury in air at normal atmospheric pressure.
  • the saturation or dew point temperature for heptane at this concentration is approximately -16° C and the saturation temperature at 10% of L.E.L. is approximately -36° C.
  • solvent vapor would begin to condense at a-temperature of -16° C at atmospheric pressure.
  • the solvent vapor In passing through the compressor, the solvent vapor is compressed at the same pressure ratio as the air and since saturation temperature is a function of vapor pressure, heptane vapor will begin to condense in the heat exchanger at a temperature higher than -16° C. If the air is cooled to -16° C in the heat exchanger, a substantial part of the heptane vapor would condense before the air stream entered the expander. Additional solvent vapor would be condensed as the air cooled during expansion to nominal atmospheric pressure in the expander. With the system designed so that the temperature of the expander exhaust were nominally -36° C and the condensed solvent coalesced and separated from the air stream, the air would return to the oven at nominally 10% of L.E.L.
  • the air could then circulate through the oven until the solvent concentration reached approximately 50% of L.E.L. and then leave the oven to enter the compressor.
  • the system would operate in equilibrium, condensing out solvent at the same rate it was evaporated from the source in the oven. Similar considerations would apply to the recovery of other condensable materials.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

Recuperation de chaleur et/ou de liquide condensable d'un milieu gazeux par utilisation d'un systeme a pompe de chaleur a cycle ouvert. Le systeme de pompe de chaleur a cycle ouvert est employe pour modifier la temperature d'un gaz par compression (1), expansion (5), echange de chaleur (3), et leur combinaison, pour condenser des vapeurs desirees portees dans le milieu gazeux pour les separer du gaz. Le systeme a pompe de chaleur a cycle ouvert peut egalement etre utilise pour extraire la chaleur d'un gaz. E st aussi concernee la recuperation d'un solvant condensable et/ou de chaleur de courant gazeux utilise dans des fours de sechage (41) qui sont employes dans le traitement de materiau charge de solvant.
PCT/US1979/000976 1978-11-15 1979-11-14 Recuperation de chaleur et de liquide utilisant un systeme a pompe de chaleur a cycle ouvert WO1980001103A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
BR7908908A BR7908908A (pt) 1978-11-15 1979-11-14 Aparelho para remocao de vapor condensavel de um gas, de vapor condensado de um gas, sistema de estufa de secagem em combinacao com o dito aparelho e processo para a separacao de vapor condensado de um gas; aparelho para a recuperacao de calor, processo e sistema de estufa de secagem em combinacao com o dito aparelho
DE7979901646T DE2967226D1 (en) 1978-11-15 1979-11-14 Heat and liquid recovery using open cycle heat pump system

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US05/960,774 US4295282A (en) 1978-11-15 1978-11-15 Heat and liquid recovery using open cycle heat pump system
US960774 1978-11-15

Publications (1)

Publication Number Publication Date
WO1980001103A1 true WO1980001103A1 (fr) 1980-05-29

Family

ID=25503606

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1979/000976 WO1980001103A1 (fr) 1978-11-15 1979-11-14 Recuperation de chaleur et de liquide utilisant un systeme a pompe de chaleur a cycle ouvert

Country Status (5)

Country Link
US (1) US4295282A (fr)
EP (1) EP0020645B1 (fr)
JP (1) JPS55500998A (fr)
DE (1) DE2967226D1 (fr)
WO (1) WO1980001103A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2491768A1 (fr) * 1980-10-14 1982-04-16 Lohmann Gmbh & Co Kg Procede et installation pour la recuperation de solvants
EP0081558A1 (fr) * 1981-06-15 1983-06-22 Minnesota Mining & Mfg Procede et dispositif de recuperation de vapeur.
FR2544992A1 (fr) * 1983-04-29 1984-11-02 Alsthom Atlantique Installation de sechage d'un produit liquide
EP0372444A1 (fr) * 1988-12-06 1990-06-13 Babcock Textilmaschinen GmbH Procédé de séchage sans émissions de bandes de textile ou analogues
CN113945086A (zh) * 2021-10-15 2022-01-18 青岛海尔空调电子有限公司 用于控制热泵烘干机的方法及装置、电子设备、存储介质

Families Citing this family (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5253432A (en) * 1988-06-30 1993-10-19 Imatran Voima Oy Drying method in a power-plant process and dryer used in the method
US4982512A (en) * 1989-12-11 1991-01-08 Jvc Magnetics America Co. Vapor recovery system
US5163980A (en) * 1991-10-22 1992-11-17 Kovach J Louis Water removal from humid gases laden with organic contaminants by series adsorption
US5249358A (en) * 1992-04-28 1993-10-05 Minnesota Mining And Manufacturing Company Jet impingment plate and method of making
US5317805A (en) * 1992-04-28 1994-06-07 Minnesota Mining And Manufacturing Company Method of making microchanneled heat exchangers utilizing sacrificial cores
BR9813792A (pt) 1998-01-09 2000-10-03 Procter & Gamble Recuperação do álcool de alquila inferior a partir de uma mistura de extração
US6739142B2 (en) 2000-12-04 2004-05-25 Amos Korin Membrane desiccation heat pump
US6691428B1 (en) * 2002-08-21 2004-02-17 Aircel Corporation Air dryer
US20140318166A1 (en) * 2013-04-26 2014-10-30 Daivd R. Loebach Moisture removal system
US10174997B2 (en) 2013-04-26 2019-01-08 David R Loebach Crop drying system
US11384960B1 (en) * 2018-11-01 2022-07-12 Booz Allen Hamilton Inc. Thermal management systems

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3321930A (en) * 1965-09-10 1967-05-30 Fleur Corp Control system for closed cycle turbine
US3394555A (en) * 1964-11-10 1968-07-30 Mc Donnell Douglas Corp Power-refrigeration system utilizing waste heat
US3768271A (en) * 1971-01-19 1973-10-30 L Denis Method and plant for storing and transporting a liquefied combustible gas
DE2725252A1 (de) * 1977-06-03 1978-12-07 Kampf Maschf Erwin Anordnung zur loesungsmittelrueckgewinnung an einem trockenkanal

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE485130A (fr) *
US2409159A (en) * 1944-08-26 1946-10-08 Allis Chalmers Mfg Co Elastic fluid conditioning apparatus
GB708646A (en) * 1951-06-15 1954-05-05 Power Jets Res & Dev Ltd Improvements relating to gas turbine plant
US3027651A (en) * 1958-07-23 1962-04-03 Leybold Hochvakuum Anlagen Process and system for removing condensable vapors
FR1325852A (fr) * 1962-03-23 1963-05-03 Rateau Soc Dispositif de dessication pour gaz
NL133167C (fr) * 1963-01-08
US3686893A (en) * 1969-12-22 1972-08-29 Purdue Research Foundation Air refrigeration device
US3899099A (en) * 1973-06-21 1975-08-12 Tank Sapp Uk Ltd Inert gas system and method for tankers
US3877245A (en) * 1973-11-30 1975-04-15 Rovac Corp Air conditioner having tempering and moisture control means
US3886765A (en) * 1974-07-29 1975-06-03 Rovac Corp Compressor-expander having thermal isolation and adjustment features
CH1666774A4 (fr) * 1974-12-16 1977-01-31
JPS52111874A (en) * 1976-03-17 1977-09-19 Hitachi Plant Eng & Constr Co Ltd Deodorization of waste gas
SE402935B (sv) * 1976-12-10 1978-07-24 Projectus Ind Produkter Ab Sett att medelst varmluft eller annan gas torka maskindetaljer samt anordning for genomforande av settet
DE2713028A1 (de) * 1977-03-24 1978-09-28 Maschf Augsburg Nuernberg Ag Verfahren und anlage zum abscheiden von wasser aus feuchtem gas

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3394555A (en) * 1964-11-10 1968-07-30 Mc Donnell Douglas Corp Power-refrigeration system utilizing waste heat
US3321930A (en) * 1965-09-10 1967-05-30 Fleur Corp Control system for closed cycle turbine
US3768271A (en) * 1971-01-19 1973-10-30 L Denis Method and plant for storing and transporting a liquefied combustible gas
DE2725252A1 (de) * 1977-06-03 1978-12-07 Kampf Maschf Erwin Anordnung zur loesungsmittelrueckgewinnung an einem trockenkanal
US4185397A (en) * 1977-06-03 1980-01-29 Hutzenlaub Armin S P Arrangement for the drying of solvent at a drying channel

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP0020645A4 *

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2491768A1 (fr) * 1980-10-14 1982-04-16 Lohmann Gmbh & Co Kg Procede et installation pour la recuperation de solvants
EP0081558A1 (fr) * 1981-06-15 1983-06-22 Minnesota Mining & Mfg Procede et dispositif de recuperation de vapeur.
EP0081558A4 (fr) * 1981-06-15 1985-12-05 Minnesota Mining & Mfg Procede et dispositif de recuperation de vapeur.
FR2544992A1 (fr) * 1983-04-29 1984-11-02 Alsthom Atlantique Installation de sechage d'un produit liquide
EP0372444A1 (fr) * 1988-12-06 1990-06-13 Babcock Textilmaschinen GmbH Procédé de séchage sans émissions de bandes de textile ou analogues
CN113945086A (zh) * 2021-10-15 2022-01-18 青岛海尔空调电子有限公司 用于控制热泵烘干机的方法及装置、电子设备、存储介质

Also Published As

Publication number Publication date
EP0020645B1 (fr) 1984-09-19
JPS55500998A (fr) 1980-11-20
US4295282A (en) 1981-10-20
EP0020645A1 (fr) 1981-01-07
DE2967226D1 (en) 1984-10-25
EP0020645A4 (fr) 1981-10-13

Similar Documents

Publication Publication Date Title
US4539816A (en) Heat and liquid recovery using open cycle heat pump system
AU552970B2 (en) Vapor recovery method and apparatus
US4295282A (en) Heat and liquid recovery using open cycle heat pump system
US4182659A (en) Method of concentrating a water-containing glycol
CA1193570A (fr) Methode d'evaporation a recuperation de vapeur pour reduire la consommation d'energie
US5152812A (en) Recovery of condensable organic compounds from inert gas streams laden
US4898599A (en) Desiccant gas drying system
EP0523929B1 (fr) Système de récupération par adsorption et condensation
EP1524019A1 (fr) Procede servant a retirer l'eau contenue dans un solide au moyen d'un materiau liquide
US20230277982A1 (en) Hybrid low dew point compressed air dryer
US4294590A (en) Removal of undesired gaseous components from hot waste gases
FI74619C (fi) Foerfarande och anlaeggning foer aotervinning av loesningsmedel.
EP4259309A1 (fr) Système et procédé de capture de dioxyde de carbone à faible consommation de ressources
WO2005030367A1 (fr) Procede ameliore de separation de gaz d'un melange gazeux et dispositif d'application d'un tel procede
JPH04326901A (ja) 溶剤回収装置
US4478686A (en) Process and apparatus for recovery of solvents
EP0346379A1 (fr) Procede de recuperation de composes volatils dans l'atmosphere
KR900017641A (ko) 공기-증기 혼합물로 부터 탄화수소 또는 화학물질 증기를 제거시키기 위한 시스템 및 방법
CA1192145A (fr) Methode et dispositif de captage de vapeurs
JPH0515725A (ja) 溶剤濃縮回収装置
EP3500353B1 (fr) Appareil et procede de desublimation d'un compose cible tel que le dioxyde de carbone ou l'anhydride phtalique
JPH0127768B2 (fr)
JPH0515724A (ja) 溶剤濃縮回収装置
US10401087B1 (en) Process for separating solvent from spent oil sand solids using superheated steam
CA3007554C (fr) Procede de separation de solvant des solides de sables bitumineux uses au moyen de vapeur surchauffee

Legal Events

Date Code Title Description
AK Designated states

Designated state(s): BR JP SU

AL Designated countries for regional patents

Designated state(s): CH DE FR GB SE